Preparation of liquid dispersions

ABSTRACT

A process for mixing or dispersing liquids is provided that includes introducing liquids to be mixed or dispersed into a mixing device having a cylindrical support. The cylindrical support includes an inlet nozzle having a bore which is in fluid communication through a turbulence chamber with a bore of an outlet nozzle, wherein the bores of the nozzles are axially spaced apart relative to one another. The liquids are then allowed to enter the turbulence chamber through the bore of the inlet nozzle where the liquids are mixed or dispersed. The mixed or dispersed liquid is then recovered from the outlet nozzle. Various devices for mixing or dispersing liquids are also provided.

FIELD OF THE INVENTION

[0001] The present invention provides a process for mixing or dispersingliquids. In particular, a process for the production of a finely dividedliquid dispersion is provided, as well as mixing devices for carryingout the process.

BACKGROUND OF THE INVENTION

[0002] European Patent Publication EP 0776 997 A1 describes a method forthe production of a finely divided dispersion of solids in which apre-dispersion is pumped through one or more slotted nozzles. Theparticle size of the dispersed phase lies in the region of 0.01 μm to 20μm. The diameter of the nozzle bore is 0.05 mm to 1 mm. The ratio ofbore length to bore diameter is 1:1 to 1:10. A preferred combinationincludes a device which has two nozzle bodies with the nozzles lyingopposite their outlet. Also described are devices in which the crudedispersion or pre-dispersion is pumped through two or more nozzleshaving an equal or decreasing bore diameter. The slotted nozzle suitablyconsists of a ceramic material, for example, zirconium oxide, or a metalcoated with ceramic.

[0003] International Patent Publication WO 97/17946 describes a methodfor the production of a liposome dispersion in which an aqueouspre-dispersion of one or more amphiphilic substances is pumped at 600bar to 900 bar through at least one homogenizing nozzle having adiameter of 0.1 mm to 0.5 mm. The homogenizing nozzle has an inletchannel and an outlet channel and includes a hard ceramic plate, inwhich the bore is situated, pressed in a steel body. The inlet channeland the outlet channel are also incorporated in the steel body. Whenseveral nozzles are used, they are arranged opposite to each other andhave a parallel inflow. The pre-dispersion is pumped in the circuitthrough the homogenizing nozzle until the average particle size of theliposome dispersion is between about 35 nm and about 80 nm.

SUMMARY OF THE INVENTION

[0004] The devices described above suffer from the drawback thatintermixing is often inefficient or incomplete. Moreover, such devicesrequire high amounts of energy to achive viable levels of intermixing.

[0005] Accordingly, it would be desirable to provide a method for mixingor dispersing liquids which permits an improved intermixing with lowerenergy expenditure compared with the state of the art.

[0006] One embodiment of the invention is a process for mixing ordispersing liquids that includes introducing liquids to be mixed ordispersed into a mixing device having a cylindrical support. Thecylindrical support includes an inlet nozzle having a bore which is influid communication through a turbulence chamber with a bore of anoutlet nozzle, wherein the bores of the nozzles are axially spaced apartrelative to one another. The liquids then enter the turbulence chamberthrough the bore of the inlet nozzle where the liquids are subjected toturbulence, i.e., are mixed or dispersed. The mixed or dispersed productis thereafter recovered from the outlet nozzle.

[0007] Another embodiment of the present invention is a mixing devicehaving a cylindrical support. The cylindrical support includes an inletnozzle having a bore which is in fluid communication through aturbulence chamber with a bore of an outlet nozzle, wherein the bores ofthe nozzles are axially spaced apart relative to one another.

[0008] Another embodiment of the invention is a scale up arrangementwherein a plurality of nozzles are disposed within the cylindricalsupport.

[0009] A further embodiment of the invention is a scale up arrangementthat includes a first support disk, a turbulence chamber, and a secondsupport disk, which are positioned in sequence in a conduit. The firstsupport disk consists of a plurality of inlet nozzles having a borediameter of about 0.05 mm to about 1 mm. The second support diskcontains a plurality of outlet nozzles having a bore diameter of about0.05 mm to about 1 mm. The bores of the inlet nozzles are in fluidcommunication with the bores of the outlet nozzles through theturbulence chamber and the bores of the inlet nozzles and outlet nozzlesare axially spaced apart relative to one another.

BRIEF DESCRIPTION OF THE DRAWINGS

[0010]FIG. 1 shows a flow diagram for carrying out the process inaccordance with the invention.

[0011]FIG. 2 shows a cross section through a mixing device in accordancewith the invention having an inlet nozzle and an outlet nozzle.

[0012]FIG. 3 shows a perspective view of the mixing device in accordancewith the invention.

[0013] FIGS. 4(a-c) shows a scale up arrangement.

[0014]FIG. 5 shows another a scale up arrangement.

DETAILED DESCRIPTION OF THE INVENTION

[0015] The present invention solves the problem of the previouslydescribed devices by pumping the liquids to be mixed or to be dispersedat temperatures of about 20° C. to about 250° C., preferably of about20° C. to about 200° C., and pressures of about 50 bar to about 2500bar, preferably of about 100 bar to about 800 bar, through a mixingdevice which consists of one or more inlet nozzles, one or moreturbulence chambers and one or more outlet nozzles, with the inletnozzle(s), turbulence chamber(s) and outlet nozzle(s) being pressed insequence in a cylindrical support. The bores of the inlet nozzles are influid communication with the bores of the outlet nozzles through theturbulence chamber and the bores of the inlet and outlet nozzles areaxially spaced apart relative to one another.

[0016] The process of the invention is especially suitable for theproduction of finely divided dispersions having average particle sizesof about 10 nm to about 1000 nm, preferably of about 50 nm to about 400nm.

[0017] For the production of liquid dispersions, a pre-emulsion ispumped through the aforementioned mixing device (dispersing unit). Thepre-emulsion is at temperatures of about 20° C. to about 250° C.,preferably of about 20° C. to about 200° C., and pressures of about 50bar to about 2500 bar, preferably of about 100 bar to about 800 bar.

[0018] The residence time of the liquids to be mixed or to be dispersedin the mixing device is about 10⁻⁶ sec to about 10⁻¹ sec.

[0019] As used herein, the term “pre-emulsion” denotes one of thefollowing systems:

[0020] a) oil-in-water emulsion (O/W emulsion);

[0021] b) water-in-oil emulsion (W/O emulsion);

[0022] c) oil-in-water emulsion in which a lipophilic active substanceis dissolved in the oil; and

[0023] d) water immiscible solvent-in-water emulsion in which alipophilic active substance is dissolved in this solvent.

[0024] An oil-in-water emulsion in which the viscosity of the dispersedphase is about 0.01 mPas to about 10,000 mPas, preferably about 0.1 mPasto about 2000 mPas, is preferred.

[0025] As used herein, the term “lipophilic active substance” includesvitamins A, D, E and K, carotenoids, and food additives, such as PUFAs(polyunsaturated fatty acids) and tocotrienols.

[0026] In the production of the pre-emulsion, the liquid to be dispersedis preferably stirred into an aqueous emulsifier solution, optionallywhile warming.

[0027] The processes for the production of finely divided liquiddispersions set forth herein relate not only to processes used in thefood manufacturing field in which food emulsifiers are used, but also ingeneral industrial dispersion processes in which correspondingindustrial emulsifiers are used. Processes which are used in the foodmanufacturing field are preferred.

[0028] In the present invention, suitable emulsifiers/stabilizers fordispersions which may be added to foods include, for example, ascorbylpalmitate, lecithins, polysorbates, sugar esters, fatty acid esters,citric acid esters, sorbitol stearates; as well as colloids, for examplegelatines and fish gelatines; carbohydrates, for example starches andstarch derivatives such as dextrin, pectin or gum arabic; milk proteinsand plant proteins. Mixtures of the aforementioned substances can alsobe used. Ascorbyl palmitate, fish gelatines or starch derivatives arepreferred, with ascorbyl palmitate being especially preferred.

[0029] Suitable industrial emulsifiers are, for example, lauryl ethyleneoxide (LEO)-9 and (LEO)-10.

[0030] The process in accordance with the invention is especiallysuitable for the production of liquid dispersions from oils, such as,for example, corn oil, palm oil, sunflower oil, and the like. Thepresent process may also be used to produce liquid dispersions fromlipophilic active substances, such as, for example, from vitamin A, D,E, and K, from carotenoids or from food additives such as PUFAs andtocotrienols.

[0031] In the present invention, suitable carotenoids include, forexample, beta-carotene, beta-apo-4′-carotenal, beta-apo-8′-carotenal,beta-apo-12′-carotenal, beta-apo-8′-carotenoic acid, astaxanthin,canthaxanthin, zeaxanthin, cryptoxanthin, citranaxanthin, lutein,lycopene, torularodin aldehyde, torularodin ethyl ester,neurosporaxanthin ethyl ester, zetacarotene, dehydroplectania-xanthinand the like.

[0032] The aforementioned lipophilic active substances may be useddirectly insofar as they are oily substances. Solid active substances,for example carotenoids, may also be used in dissolved form in oil or inwater-immiscible solvents.

[0033] Suitable water-immiscible solvents that may be used in thepresent invention include halogenated aliphatic hydrocarbons, such asfor example, methylene chloride, water-immiscible esters, such ascarboxylic acid dimethyl ester (dimethyl carbonate), ethyl formate,methyl, ethyl or isopropyl acetate; or water-immiscible ethers such asfor example, methyl tert.butyl ether, and the like.

[0034] The process in accordance with the invention provides a veryefficient mixing or dispersing process for liquids. The mixing ordispersing process in accordance with the invention is also suitable forperforming chemical reactions having very short reaction times, forexample on the order of seconds or fractions of seconds.

[0035] The mixing device in accordance with the invention has, incontrast to the known devices described above, an arrangement of thebores of the inlet and outlet nozzles which is axially spaced apartrelative to one another. Thus, by the turbulence chamber beingpositioned between the nozzles, the short term stability of mixtures,especially of dispersions, is increased. This results in a liquiddispersion that is homogenized more strongly.

[0036] In FIG. 1, a supply container (1) is followed by a high pressurepump (2) which is optionally connected to a heat exchanger (3). Themixing device (4) is positioned thereafter.

[0037]FIG. 2 and FIG. 3 show a mixing device (4) consisting of an inletnozzle (6) having a bore diameter of about 0.05 mm to about 1 mm,preferably about 0.05 mm to about 0.5 mm; a turbulence chamber (7)having a diameter of about 0.5 mm to about 10 mm, preferably about 1 mmto about 10 mm, such as about 1 mm to about 5 mm; an outlet nozzle (8)having a bore diameter of about 0.05 mm to about 1.5 mm, preferablyabout 0.05 mm to about 0.8 mm, with the inlet nozzle (6), the turbulencechamber (7) and the outlet nozzle (8) being pressed in sequence in acylindrical support (5). The inlet nozzle is in fluid communication withthe outlet nozzle via the turbulence chamber. The bores of the nozzlesare axially spaced apart relative to one another.

[0038] As used herein, the phrase “fluid communication” is intended tomean that liquids to be mixed or dispersed enter the turbulence chamberthrough the bore of the inlet nozzle. Once in the turbulence chamber,the liquids are mixed and then exit the chamber via the bore of theoutlet nozzle.

[0039] In the present invention, the bores of the nozzles are said to beaxially spaced apart relative to one another. Thus, as FIG. 2 indicates,the bores of the inlet and outlet nozzles are positioned on oppositesides of the axis of the chamber.

[0040] The ratio of length to diameter of each nozzle bore amounts inthe case of the inlet nozzle or the outlet nozzle to about 1 to 10,preferably about 1 to 5.

[0041] The ratio of length to diameter of the turbulence chamber isabout 0.5 to about 50, preferably about 0.5 to about 20, such as about0.5 to about 10.

[0042] The diameter of the turbulence chamber must be greater than thediameter of the outlet nozzle.

[0043] The bore diameters of the inlet nozzle and the outlet nozzle maybe the same or different. However, an embodiment in which the borediameter of the inlet nozzle is smaller than the bore diameter of theoutlet nozzle is preferred. For example, the bore diameter of the inletnozzle is about 0.2 mm and the bore diameter of the outlet nozzle isabout 0.25 mm.

[0044] The nozzles are suitably manufactured from wear-resistantmaterials such as e.g. sapphire, diamond, stainless steel, ceramic,silicon carbide, tungsten carbide, zirconium, and the like.

[0045] The bores of the nozzles may be round, rectangular, orelliptical. A bore which has a cone in the mouth is also suitable.

[0046] The cylindrical support (5) likewise consists of wear-resistantmaterials, suitably of stainless steel.

[0047]FIG. 4 shows one possibility for the scale up of the mixingdevice.

[0048] Section 4 a shows a plurality of nozzles in accordance with theinvention with nozzle inserts (11), which are secured to a support plate(10). In the present invention, the nozzle inserts may be secured to thesupport plate by any conventional means, such as for example, they maybe screwed into the support plate. The support plate is positioned in aconduit (9) (cylindrical support).

[0049] Cross section 4 b shows only one nozzle insert (11′). The nozzleinsert (11′), the support plate (10) as well as the conduit (9) aremanufactured from wear-resistant materials, preferably stainless steel.

[0050] Section 4 c shows the screwable nozzle support (11″) whichcontains the nozzle (4 c) in accordance with the invention.

[0051]FIG. 5 shows another scale up arrangement. In this arrangement,the mixing device consisting of a support disk (12), a turbulencechamber (13) and a support disk (14), which are positioned in sequencein a tubular conduit (15), with the first support disk (12) containing aplurality of inlet nozzles (16) having a bore diameter of about 0.05 mmto about 1 mm, preferably about 0.05 mm to about 0.5 mm, and the secondsupport disk (14) containing a plurality of outlet nozzles (17) having abore diameter of about 0.05 mm to about 1 mnm, preferably about 0.05 mmto about 0.8 mm. The bores of the inlet nozzles are in fluidcommunication with the bores of the outlet nozzles through theturbulence chamber and the bores of the inlet nozzles and outlet nozzlesare axially spaced apart relative to one another.

[0052] The number of nozzles determines the diameter of the turbulencechamber (13). The ratio of length to diameter of the turbulence chamberis designed such that the residence time of a liquid to be dispersed inthe dispersing unit is about 10⁻⁶ sec to about 10⁻¹ sec.

[0053] As set forth in FIG. 1, for the production of a finely dividedliquid dispersion, a pre-emulsion is first produced in the supplycontainer (1) in a known manner and pumped through the dispersing unit(4) at temperatures of about 20° C. to about 250° C., preferably about20° C. to about 200° C., and pressures of about 50 bar to about 2500bar, preferably about 50 bar to about 800 bar, using a high pressurepump (2). Where required, the pre-emulsion may be heated for a briefperiod in the heat exchanger (3). The residence time of the liquid to bedispersed in the dispersing unit (4) is about 10⁻⁶ sec to about 10⁻¹sec.

[0054] The following examples are provided to further illustrate thepresent process. These examples are illustrative only and are notintended to limit the scope of the invention in any way.

[0055] In the Examples, in addition to the food emulsifier ascorbylpalmitate, industrial emulsifiers lauryl ethylene oxide (LEO)-9 and(LEO)-10 were also used. This is a so-called “more rapid” emulsifierwhich very rapidly stabilizes newly formed phase boundaries.

EXAMPLE 1 Corn Oil and Lauryl Ethylene Oxide

[0056] The emulsion had the following composition:

[0057] 87 wt. % deionized water, 10 wt. % corn oil, and 3 wt. % laurylethylene oxide-9.

[0058] Deionized water was placed in a kettle and warmed to 40° C. Theemulsifier lauryl ethylene oxide (LEO)-9 was dissolved in the water.Subsequently, the corn oil was stirred in and comminuted with an ULTRATURRAX mixer at 1000 rpm. When the content of dispersed phase was 10 wt.%, the weight ratio of corn oil to lauryl ethylene oxide was 10:3. Thepre-emulsion was homogenized three times at a pressure of 600 bar usingthe dispersing unit set forth in FIG. 2 in accordance with theinvention. The geometric dimensions of the dispersing units used are setforth in Table 1. The particle sizes were determined in a known mannerby means of photon correlation spectroscopy.

EXAMPLE 2 Corn Oil and Ascorbyl Palmitate

[0059] Here, ascorbyl palmitate was used as the emulsifier. Thequantitative composition of the emulsion corresponded to that in Example1.

[0060] Deionized water was placed in a kettle and warmed to 40° C.Ascorbyl palmitate was dissolved in the water at pH values between sevenand eight. The production of the pre-emulsion and the homogenizationwere carried out according to Example 1.

EXAMPLE 3 dl-alpha-Tocopherol and Ascorbyl Palmitate

[0061] dl-alpha-Tocopherol and ascorbyl palmitate were combined inaccordance with Example 2.

EXAMPLE 4 dl-alpha-Tocopherol and Ascorbyl Palmitate

[0062] A pre-emulsion was produced in accordance with Example 2. Thecontent of the dispersed phase was 30 wt. %. The weight ratio ofdl-alpha-tocopherol to ascorbyl palmitate was 10:1. The pre-emulsion washomogenized once at pressures of 100 bar, 200 bar, 300 bar, 400 bar and500 bar using the dispersing unit in accordance with the invention shownin FIG. 2.

EXAMPLE 5 dl-alpha-Tocopherol, Corn Oil with Ascorbyl Palmitate and FishGelatine

[0063] An emulsion containing 65 wt. % deionized water, 6 wt. % ascorbylpalmitate, 4 wt. % fish gelatine, 18 wt. % dl-alpha-tocopherol and 7 wt.% corn oil was produced in the manner described hereinafter.

[0064] The deionized water was placed in a kettle and warmed to 60° C.The fish gelatine was dissolved in the water. Then, the ascorbylpalmitate was dissolved in the aforementioned solution at pH valuesbetween seven and eight. Subsequently, the dispersed phase includingdl-alpha-tocopherol and corn oil was stirred in as described inExample 1. The pre-emulsion was homogenized in accordance with Example4.

[0065] Examples 6-10 are comparative Examples using a single-holenozzle.

EXAMPLE 6 Corn Oil and Lauryl Ethylene Oxide

[0066] The pre-emulsion was produced in accordance with Example 1 andhomogenized three times at a pressure of 600 bar in a single-holenozzle. The single-hole nozzle had an acute angled inlet and outlet. Thegeometric dimensions of the single-hole nozzle are given in Table 1.

EXAMPLE 7 Corn Oil and Ascorbyl Palmitate

[0067] The pre-emulsion was produced in accordance with Example 2 andhomogenized in the manner described in Example 6.

EXAMPLE 8 dl-alpha-Tocopherol and Ascorbyl Palmitate

[0068] The pre-emulsion was produced in accordance with Example 3 andhomogenized in the manner described in Example 6.

EXAMPLE 9 dl-apha-Tocopherol and Ascorbyl Palmitate

[0069] The pre-emulsion was produced in accordance with Example 4 andhomogenized once in a single-hole nozzle as described in Example 6 atpressures of 100 bar, 200 bar, 300 bar, 400 bar and 500 bar. Theparticle size was determined in a known manner by means of laserdiffraction spectrometry and photon correlation spectroscopy.

EXAMPLE 10 dl-alpha-Tocopherol, Corn Oil with Ascorbyl Palmitate andFish Gelatine

[0070] The pre-emulsion was produced in accordance with Example 5 andhomogenized once in a single-hole nozzle as described in Example 6 atpressures of 100 bar, 200 bar, 300 bar, 400 bar and 500 bar. TABLE 1Geometric dimensions of the dispersing units used. Length Bore diameterBore diameter of the Bore diameter of the of the turbulence of theNozzle inlet nozzle turbulence chamber outlet nozzle type [mm] chamber[mm] [mm] [mm] Nozzle I 0.2 2 1.5 0.25 Nozzle I 0.2 2 3 0.28 long NozzleII 0.2 2 1.5 0.2 Single- 0.2 — — — hole nozzle

[0071] The average particle sizes of the finely divided liquiddispersions of Examples 1-6 are set forth in Tables 2 and 3. TABLE 2Average particle sizes in nm of experiments 1, 2, 3, 6, 7 and 8. Passage1 Passage 2 Passage 3 Example Nozzle type Particle size Particle sizeParticle size 1 Nozzle I 218 202 202 0.2/0.25 mm 219 215 200 1 Nozzle II230 214 212 0.2/0.2 mm 231 220 208 6 single-hole 307 256 247 nozzle 298250 248 0.2 mm 2 Nozzle I 275 250 238 0.2/0.25 mm 2 Nozzle II 294 266245 0.2/0.2 mm 7 single-hole 340 320 275 nozzle 0.2 mm 3 Nozzle I 295287 267 0.2/0.25 mm 3 Nozzle II 312 294 302 0.2/0.2 mm 8 single-hole 442416 403 nozzle 0.2 mm

[0072] From Table I it is evident that the homogenization using nozzlesI and II in accordance with the invention produces a liquid dispersionwith a smaller particle size compared with the homogenization using asingle-hole nozzle. When nozzles I and II are used, particle sizes up toa third smaller are produced compared with the single-hole nozzle.

[0073] The best homogenization takes place in nozzle I. Here, theparticle size was reduced to 200 nm after a triple homogenization. Thevalues from Example 1 reveal that the reproducibility of the results isalso good.

[0074] The average particle sizes of the finely divided liquiddispersions obtained in Examples 4, 5, 9, and 10 are set forth in Table3. TABLE 3 Average particle sizes in nm of experiments 4, 5, 9 and 10.100 bar 200 bar 300 bar 400 bar 500 bar Particle Particle ParticleParticle Particle Nozzle size size size size size Ex. type [nm] [nm][nm] [nm] [nm] 4 Nozzle I 1800 1370 1400 1105 1080 0.2/0.25 nm 4 NozzleI/ 1370 740 745 660 600 long 0.2/0.28 mm 9 Single-hole 5200 3080 15201370 914 nozzle 0.2 mm 5 Nozzle I 435 410 340 350 345 0.2/0.25 mm 5Nozzle I/ 420 410 360 325 290 long 0.2/0.28 mm 10 Single-hole 440 430360 350 355 nozzle 0.2 mm

[0075] From Table 3 it is evident that the homogenization using nozzle Iand nozzle I/long produce liquid dispersions with a smaller particlesize than the homogenization using a single-hole nozzle. The besthomogenization takes place using nozzle I/long.

[0076] The invention being thus described, it will be obvious that thesame may be varied in many ways. Such variations are not to be regardedas a departure from the spirit and scope of the invention, and all suchmodifications are intended to be included within the scope of thefollowing claims.

We claim:
 1. A process for mixing or dispersing liquids comprising: (a) introducing liquids to be mixed or dispersed into a mixing device having a cylindrical support comprising an inlet nozzle having a bore which is in fluid communication through a turbulence chamber with a bore of an outlet nozzle, wherein the bores of the nozzles are axially spaced apart relative to one another; and (b) allowing the liquids to enter the turbulence chamber through the bore of the inlet nozzle where the liquids are mixed or dispersed.
 2. A process according to claim 1 further comprising heating the liquids to be mixed or dispersed to a temperature of about 20° C. to about 250° C. at a pressure of about 50 bar to about 2500 bar prior to distributing the liquid through the mixing device.
 3. A process according to claim 2 further comprising heating the liquids to be mixed or dispersed to a temperature of about 20° C. to about 200° C. at a pressure of about 100 bar to about 800 bar.
 4. A process according to claim 1 wherein the liquids are pumped into the bores of the inlet nozzle.
 5. A process according to claim 1 wherein a residence time of the liquids to be mixed or to be dispersed in the mixing device is about 10⁻⁶ sec to about 10⁻¹ sec.
 6. A process according to claim 1 wherein a liquid dispersion having an average particle size of about 10 nm to about 1000 nm is produced.
 7. A process according to claim 6 wherein a liquid dispersion having an average particle size of about 50 nm to about 400 nm is produced.
 8. A process according to claim 1 wherein a pre-emulsion is pumped through the mixing device at a temperature of about 20° C. to about 200° C. and a pressure of about 50 bar to about 2500 bar.
 9. A process according to claim 8 wherein the pre-emulsion is pumped through the mixing device at a temperature of about 20° C. to about 200° C. and a pressure of about 100 bar to about 800 bar.
 10. A process according to claim 8, wherein the pre-emulsion is an oil-in-water emulsion wherein a viscosity of a dispersed phase of the emulsion is about 0.01 mPas to about 10,000 mPas.
 11. A process according to claim 10 wherein the viscosity of the dispersed phase of the emulsion is about 0.1 mPas to about 2000 mPas.
 12. A process according to claim 8 wherein the pre-emulsion is produced by stirring the liquid to be dispersed into an aqueous emulsifier solution, optionally while warming.
 13. A process according to claim 12 wherein the emulsifier is ascorbyl palmitate.
 14. A process according to claim 1 wherein the liquid to be dispersed is an oil or a lipophilic active substance.
 15. A process according to claim 1 wherein a lipophilic active substance is mixed or dispersed into a liquid in the mixing device.
 16. A process according to claim 15 wherein the lipophilic active substance is selected from the group consisting of vitamin A, vitamin D, vitamin E, vitamin K, carotenoids, food additives, and mixtures thereof.
 17. A process according to claim 16 wherein the food additive is selected from the group consisting of polyunsaturated fatty acids, tocotrienols, and mixtures thereof.
 18. A mixing device having a cylindrical support comprising an inlet nozzle having a bore which is in fluid communication through a turbulence chamber with a bore of an outlet nozzle, wherein the bores of the nozzles are axially spaced apart relative to one another.
 19. A mixing device according to claim 18 wherein a bole diameter of the inlet nozzle is about 0.05 mm to about 1 mm, a diameter of the turbulence chamber is about 0.5 mm to about 10 mm, and a bore diameter of the outlet nozzle is about 0.05 mm to about 1.5 mm.
 20. A mixing device according to claim 19 wherein a bore diameter of the inlet nozzle is about 0.05 mm to about 0.5 mm, a diameter of the turbulence chamber is about 1 mm to about 5 mm, and a bore diameter of the outlet nozzle is about 0.05 mm to about 0.8 mm.
 21. A mixing device according to claim 18 wherein a bore diameter of the inlet nozzle is smaller than a bore diameter of the outlet nozzle.
 22. A mixing device according to claim 18 wherein the inlet and outlet nozzles are manufactured from a material selected from the group consisting of sapphire, diamond, stainless steel, ceramic, silicon carbide, tungsten carbide, and zirconium oxide.
 23. A mixing device according to claim 18 wherein a length to diameter ratio of the inlet and outlet nozzle bores is about 1 to about 10, preferably about 1 to about
 5. 24. A mixing device according to claim 18 wherein a length to diameter ratio of the inlet and outlet nozzle bores is about 1 to about
 5. 25. A mixing device according to claim 18 wherein a length to diameter ratio of the turbulence chamber is about 0.5 to about
 50. 26. A mixing device according to claim 25 wherein the length to diameter ratio of the turbulence chamber is about 0.5 to about
 20. 27. A mixing device according to claim 26 wherein the length to diameter ratio of the turbulence chamber is about 0.5 to about
 10. 28. A mixing device according to claim 18 wherein a diameter of the turbulence chamber is greater than a diameter of the outlet nozzle.
 29. A nozzle for use in the mixing device of claim 18 comprising a plurality of nozzle inserts secured to a support plate, the nozzle being disposed within the cylindrical support.
 30. A mixing device comprising a first support disk, a turbulence chamber, and a second support disk, which are positioned in sequence in a conduit, the first support disk consisting of a plurality of inlet nozzles having, a bore diameter of about 0.05 mm to about 1 mm, and the second support disk containing a plurality of outlet nozzles having a bore diameter of about 0.05 mm to about 1 mm, wherein the bores of the inlet nozzles are in fluid communication with the bores of the outlet nozzles through the turbulence chamber and the bores of the inlet nozzles and outlet nozzles are axially spaced apart relative to one another.
 31. A mixing device according to claim 30 wherein the bore diameters of the inlet nozzles are about 0.05 mm to about 0.5 mm and the bore diameters of the outlet nozzles are about 0.05 mm to about 0.8 mm.
 32. A mixing device according to claim 30 wherein a plurality of liquids are mixed therein.
 33. A mixing device according to claim 30 wherein a plurality of liquids are mixed in seconds or fractions of seconds.
 34. A mixing device according to claim 30 wherein chemical reactions with very short reaction times in the region of seconds or fractions of seconds are performed. 